WO2008039400A1 - Gazéificateurs à carburant de masse - Google Patents

Gazéificateurs à carburant de masse Download PDF

Info

Publication number
WO2008039400A1
WO2008039400A1 PCT/US2007/020555 US2007020555W WO2008039400A1 WO 2008039400 A1 WO2008039400 A1 WO 2008039400A1 US 2007020555 W US2007020555 W US 2007020555W WO 2008039400 A1 WO2008039400 A1 WO 2008039400A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasifier
shell
gas
slag
circulating
Prior art date
Application number
PCT/US2007/020555
Other languages
English (en)
Inventor
Lloyd E. Weaver
Original Assignee
Lew Holdings, Llc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lew Holdings, Llc filed Critical Lew Holdings, Llc
Priority to US12/442,215 priority Critical patent/US20100107493A1/en
Publication of WO2008039400A1 publication Critical patent/WO2008039400A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/40—Gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste
    • F23G2209/261—Woodwaste

Definitions

  • This invention relates generally to gasifiers.
  • Two types of gasifiers are bulk fuel fed and entrained flow fed. Entrained flow fed gasifiers require more fuel processing such as pulverizers and slurring of coal, for example. Entrained flow also requires other extra equipment such as blowers and bag house. This extra fuel preparation increases the cost and complexity of the gasifier and also lowers reliability. Entrained flow gasifiers also tend to be very large and cumbersome, with present reliability so poor that two gasifiers are frequently supplied to do the job of one.
  • Down draft gasifiers typically employ a co-current process in which tars are burned off and converted into a gas before exiting the process.
  • down draft gasifiers generally have been limited to low fuel moisture levels because there was no method to dry the fuel within the gasifier.
  • Updraft gasifiers can gasify much wetter fuels than downdraft units, because the hot gas exits through the fresh fuel mass. But the upper gas exit temperatures are limited in updraft gasifiers by the blast flow rate and how much heat energy can be pulled upwards.
  • downdraft gasifiers maintain a large fresh fuel mass above the fire or incandescent zone that unlike updraft processes has no hot gas continually flowing through it to dry it, and like updraft needs to maintain as hot an average a fuel mass as possible to maximize the output of the gasifier.
  • a gasifier including a gasifier shell, means for introducing fuel into the shell, and means for introducing oxygenate into the shell.
  • the gasifier also includes means for discharging gas from the shell, which can be located below the means for introducing oxygenate.
  • the gasifier can also include means for re-circulating gas prior to gas being discharged from the shell.
  • FIG. 1 is a side of one embodiment of a gasifier.
  • FIG. 2 is a side of an alternative embodiment of a gasifier.
  • FIG. 3 is a side elevation view of a non-sticking valve useful in the gasifier of FIG. 4.
  • FIG. 4 is a partial side of an alternative gasifier.
  • FIG. 5 is a partial side of another embodiment of a gasifier.
  • FIG. 6 is a cutaway view of a portion of the wall of the gasifier of FIG. 5.
  • FIG. 7 is a side of yet another embodiment of a gasifier.
  • FIG. 1 shows one embodiment of a slagging gasifier as if it is being used in a pressurized operation, say up to thirty bar pressures.
  • Valve details and controls for de-pressurizing and re-pressurizing lock hoppers and controls are well known and are not shown. The upper and body sections are described first and are the same for each ash discharge method.
  • Lock hopper 1 is filled using a conveyor (not shown) that has a much faster capacity than the maximum usage of the gasifier.
  • Undercutting rotating inward helical front edge of self-aligning plate 2 performs the unloading function by pulling material from the outer perimeter of base 3 and under rotating cap 4.
  • the loose spline drive connection of unloader plate 2 to drive motor 6 allows plate 2 to conform perfectly to base 3 when rotating, reducing friction and eliminating binding forces.
  • Cap 4 prevents free fall of fuel or material 18 into unloader concentric opening 5.
  • materials caught in between the bottom of cap 4 and top of base 3 are broken apart by such grinding action. This is useful for unloaders unloading ash that may contain large clinkers.
  • Drive motor 6 is supported by inside braces 7 attached to the inside of the lock hopper 1.
  • Unloaded material 18 slides down through cone funnel 8 through lower lock hopper valve 9 (typically a sliding disk-type valve such as a higher temperature EverlastingTM valve) into gasifier upper zone 10 to form material level 11 , which surges up and down in level slightly as there is no feed as the hopper 1 is refilled by its high capacity conveyor (not shown).
  • Level 11 is measured by vertical sensor 12, and the level data is issued to control the speed of the drive motor 6, including using higher speeds at first after refilling the lock hopper 1 to recover level 11.
  • the gasifier includes a water cooled gasifier shell 13, and the midsection of the shell 13 has a thick, high temperature refractory 14 penetrated by at least two levels of 3000 F rated gas cooled thermocouple temperature sensors 15 and 16, steam and oxygenate (e.g., O2 or air) feed tubes 17, and a final exhaust water cooled and ceramic lined gas exit pipe 19 extending through the shell 13.
  • a combined sensor 20 mounted under the gas exit pipe 19 includes duplex thermocouples like 15 or 16 plus a CO2 sampling sensor.
  • Refractory 14 is further reinforced with a high temperature rated refractory coating 21 throughout an ash incandescent zone 22 and ash or slag removal zone discussed below.
  • Gas 23 produced in the gasifier exits by cone shaped spaces 24 through underside openings 26 of a water-cooled and lined torus shaped pipe 25 mounted inside the gasifier shell 13 and passes out through the exit pipe 19, which is in fluid communication with the torus shaped pipe 25.
  • Intense gasification within incandescent zone 22 feeds gas down through a cone volume 27 formed by an extra high temperature refractory, torus-shaped nose 28 mounted on the torus shaped pipe 25 and a cone solid 29 centered with respect to the torus.
  • the gas 23 passing through this space and up though cone shaped spaces 24 completes the reduction reactions that burn off tars to make a tar free gas for subsequent filtering prior to other operations.
  • a lower slag rejection space 30 is defined by the extra high temperature refractory 14 and refractory coatings 21.
  • the cone solid 29 is located across the top of an inclined, refractory disk 31 (inclined at about three degrees) that is supported on it perimeter at 33 and by posts 34.
  • Molten slag flow 32 passes through notches 35 molded in refractory disk 31 around support posts 34 to enter a tap hole 36 which at the top has an optional inductive copper coil 37 to melt slag at the tap hole 36 as needed and is fed power and water coolant at 38 and which exits as water and power connection 39. Coolant flow is constant to insure copper coil 37 doesn't melt.
  • inductive power would not be used unless tap hole 36 is plugged which can be determined by the failure of the slag lock hopper 44 to fill. Plugging of the tap hole 36 is also unlikely if the incandescent temperature of zone 22 is maintained sufficient as measured by the temperature sensor 16. Leaving tap hole 36, the slag 32 enters a quenching vessel 40 with maintained water level 41 and having an optional slag grinder 42, which should not be needed if a fast unloader is added to the slag lock hopper. Details of a water system to fill the vessel 40 are not shown but are well known in the art.
  • Slag 32 flows through a valve 43 (such as an EverlastingTM valve) into the slag lock hopper 44, which will typically have a slag rejection valve (not shown) that is similar to the valve 43.
  • Steam 45 from quenching the slag 32 rises to combine with exit gas 23.
  • Water flow control to replenish the water level 41 of the quench vessel 40 is not shown and is well known in the art.
  • the cone volume 27 is filled with chunk sized stove wood up to the feed tubes 17, and the shell 13 is then filled with coal to level 11.
  • An igniter burner (not shown) is inserted into the feed tube 17 to ignite the wood coal area, then oxygenate blast flow is ramped up.
  • igniters can be permanently built into the feed tube 17.
  • the exit pipe 19 being located below the feed tubes, and thus below the incandescent zone 22, the gasifier provides a co-current process that burns off tars before the exit gas 23 is discharged. In other words, the fuel 18 and the gas 23 flow in essentially the same direction through the interior of the shell 13.
  • FIG. 2 an alternative approach for dry ash removal, that is still capable of pressurized operation, is described.
  • the feed and body of the gasifier is the same as described above, so just the ash removal section will be described here.
  • This is a lower temperature version of the gasifier whereby the temperatures maintained in the incandescent zone 22 are maintained below slagging conditions, or generally under 2300F.
  • the ash unloader has a raised solid high strength refractory cone 46 around which the gas 23 passes to insure tars are burned off.
  • the design rules of thumb for sufficient incandescent zone plus following volumes and gas retention time for fuel to gasify and burn off tars discussed above in connection with FIG. 1 also apply to this lower temperature dry ash process.
  • a drive gearhead 47 rotates cone 46 and its supporting disk 49 which will support any ash or clinkered mass that falls within this space and which are broken up by all rotating members. Because of wear and because it is a hot area, cone 49 is coated with high temperature silicon carbide or has other wear and heat resistant inserts on its top surface so as to withstand this severe duty. Also, rotating elements are water cooled which helps prolong their life. Construction of such rotating ash unloading conical structures has the advantage that it is solid and water cooled which should prolong its life even more. Also, a thicker helical front face can be specified which enables the ash unloading assembly to rotate even slower.
  • Ash and/or clinkers 50 accumulate and rest on independently water-cooled support base 51, cooled by water inflows and outflows 53 and 54, respectively.
  • a center hole 52 is provided for ash discharge through right angle cone transition piece 55 through a high temperature valve 56 to a lock hopper vessel 57 (partially shown).
  • An ash proximity sensor 58 such a nuclear gage or air cooled point-type reflective gages, could be used with sample-data control algorithms used to maintain a constant speed to the unloader drive, maintains a nearly constant bed of ash level within the this space. In the case of the nuclear sensors, they are offside so as to only measure ash or slag materials, but not the center cone 46.
  • the lock hopper 57 While the lock hopper 57 empties, some ash may accumulate atop closed valve 56, but also the rotation of unloader helix 64, which rotates with the disk 49 and the cone 46 respectively, may be momentarily stopped until hopper unloading is complete.
  • the lock hopper 57 may also have an unloader (not shown) to quickly discharge ash to atmosphere. Coolant for drive shaft 61 and support bearing/seal 62 is fed coolant water in at 58 and out at 59 through rotary valve 60. The same coolant travels up and down shaft 61 and is fed in and out of floating unloading helix 64 through high temperature metallic covered hoses 65. Water ash quenching in the lock hopper 57 could be used if needed, which adds steam flow to the outlet gas 23.
  • ash is filled to the sensor level 58, and from there to the feed tube 17 is filled with chunk sized stove wood and then filled with wood or coal to level 11 with an igniter burner (not shown) inserted in the feed tube 17 to ignite the wood coal area and then ramp up oxygenate blast flow.
  • igniters can be built into tube 17; ash rejection is held under manual control until the chunk wood is consumed.
  • FIG. 3 depicts a high temperature disk valve with inductive heating method to unstick the valve in the event it freezes open or shut based on the molten slag that will become deposited on the valve disk surfaces as it operates.
  • the use of this valve is shown in FIG. 4 as an emergency molten slag flow shutoff valve when discharging high-pressure slag.
  • the valve is open allowing slag to continuously flow out.
  • the valve is constructed around flange 66 with actuator 67 that rotates arm 68 which rotates ceramic disk 69 to open or close discharge opening 81 formed by ceramic cylinder 77 attached to flange 66.
  • Piston 70 imbedded in disk 69 is also held within cylinder 71 attached to arm 68.
  • "O" ring 74 prevents oil from leaking by piston 70 and cylinder 71 combination.
  • disk 73 is heated to insure solidified slag either on disk 69 or disk 73 becomes molten allowing a flush non-leaking seal.
  • nonconducting cylinder 75 which has induction coil 76 surrounding it which is supported by an inside groove in outer non-conducting cylinder 75.
  • Conducting tungsten disk 73 is also supported by an inside groove in 75.
  • Air gap 78 is small to increase the heating effectiveness of coil 76 to disk 73:
  • the tungsten disk 73 can get hot enough to melt the slag to unstick the two surfaces of disk 73 and disk 69, or also melt deposited solidified slag to allow the disk 69 to slide shut and to re-seal as noted previously.
  • a heat shield 80 depicted as dashed line is attached to one side of swinging arm 68 such that when the valve is open, i.e. disk 69 swung away from opening 81, hot material 82 pouring from opening 81 will not damage actuating parts.
  • FIG. 4 depicts just the lower slag area of FIG. 1 but shows an alternative direct molten slag discharge method and control thereof without using quenching or lock hoppers.
  • the gas discharge area 92 has a constant slag level 83 as measured by a nuclear gage comprised of emitter 84 and receiver 85. They are located to measure slag depth off-side, i.e. do not detect item 104.
  • coolant in feed and out feed copper pipes to copper coils 88 and 89 respectively can also have inductive currents to melt away some of slag build-up 94 should opening 93 become frozen shut, which would cause level 83 to rise to an unacceptable level.
  • inductive coil 97 provides the needed energy which has constant coolant in-flow 98 and outflow 99, which also serve as inductive current carriers. Coolant flow maintains coil 97 protective slag coating 100 and the coil also has electrical back insulation 101 imbedded in refractory 102.
  • cone shaped riser 103 made form high temperature refractory is attached to the bottom of refractory 102.
  • Slag 104 flows under notches 105 cast in the base of cone 103 to enter the controlled tap hole opening 93 to leave as molten slag flow 95.
  • a much longer length to slag opening 93 can be created by adding more coil sections like 88 and 89 as indicated previously, and can be engineered in the base of refractory area 102 by extension of lower gasifier housing 106 such as using a pipe extension before attaching safety shutoff valve 96.
  • a longer length to opening 93 may be needed such that the viscosity change in the slag to dissipate the pressure energy will enable a lower velocity of slag flow 95 from the exit point of safety shutoff valve 96.
  • molten slag is added to reach level 83 and maintained molten with inductive energy to coil 97 while filling the remainder of the gasifier with coal to level 11 (not shown but the same level as in FIG. 1) and with an igniter burner (not shown) inserted in feed tube 17 to ignite the coal and then ramp up oxygenate blast flow.
  • igniters can be permanently built into tube 17.
  • FIG. 5 shows another embodiment of a gasifier that is similar to the gasifier of FIG. 1 but includes means for hot gas re-circulation. Ash rejection and gas out details can be the same as described in connection with the above embodiments and are thus not described here.
  • This gasifier includes an outer steel shell 5 having an insulation limit 6 and a refractory thickness limit 7.
  • an enlarged cross section of the outer steel shell 5 shows the wall thickness details.
  • Item 1 is an outer dimpled wall for a steel pressure shell 2, which provides for a water cooling method generally comprising a forced water circulating method feeding a steam drum above, details not shown but well known in the art.
  • Item 3 is the insulation next to shell 2
  • item 4 is the thick refractory, up to 14 inches thick.
  • fresh fuel 8 is fed through a lock hopper valve 9 to a controlled level 10.
  • the inclined fuel level 10 is measured with a high temperature level sensor 11, which is preferably a gas purged infrared or radar sensor but other sensors can also be used if able to withstand the temperature of the re-circulating gas 16.
  • a motorized gearhead 12 drives an agitator 13 located in the fresh fuel zone 17 via a shaft 14, which is water cooled through a rotary valve 15.
  • the agitator 13 also levelizes the fuel level 10. Note that re-circulating gas flow 16 causes gasification of the upper fuel zone 17 to start, including caking. Thus, the agitator 13 operates to break up caking and insure relatively uniform gas flows 16 up through the fuel zone 17. Extending the length of the shaft 14 and providing multiple agitating bars to the agitator 13 can increase the drying potential for downdraft units.
  • Hot, re-circulation gases 16 are pulled up from the fire or incandescent zone 18 by a rotating blower impeller 19 mounted within the inside gasifier case 20 at or near the top of the shelf 5.
  • the blower impeller 19 is mounted just inside the gasifier shell 5 within a water-cooled bower case.
  • coolant could be fed through rotary joints (not shown) to cool the impeller vanes, and a separate center pipe (not shown) could periodically feed higher pressure steam to blast clean the surfaces of the vanes.
  • blower pre-filters and tar conversion devices outside the gasifier shell 5 could be provided as well to lessen the particulate and tars loading on the blower impeller 19.
  • the output of the blower impeller 19 is fed to a hollow, torus-shaped plenum 21 in the upper zone of the gasifier shell 5, which in turn feeds hot gas down though individual ceramic vertical tubes 22 located in the wall of shell 5 around the circumference of the shell 5.
  • the pressure needed to re-circulate the gases 16 is relatively low, meaning that the gasifier does not require much energy to re-circulate the gases 16.
  • the plenum 21 could be rectangular in cross section.
  • the blower impeller 19 forces the gases 16 into the plenum 21 and down though ceramic down-flow tubes 22 to combine as gas 23 in the feed or blast tube 26 which has oxidant blast 25.
  • the fuel is dried. Accordingly, the overall downdraft process now has the advantages of updraft fuel drying plus the steam from the wet fuel is transferred to the incandescent zone 18 where it facilitates gasification reactions, reducing the amount of extra blast steam needed depending on the moisture content of the fuel.
  • the output capability of the gasifiers will be improved. Furthermore, because the gases 16 are hot, tars and particulates are minimized. Accordingly, the re-circulating gases 16 are not necessarily cleaned prior to re-circulating as gas 23 into the fire zone 18 of the gasifier, although such cleaning could be performed if desired.
  • the plenum 21 has a toroidal shape extending around the upper gasifier inner shell, as depicted by dotted line 24.
  • ash or slag removal can be accomplished in the manner described above.
  • the blower impeller 19 and the down-flow tubes 22 are located within the gasifier steel shell 5, which if pressurized more, the upper design horsepower for motor 31 increases and thickness of impeller 19 increases as gases 16 become more dense.
  • the speed of the blower impeller 19, as driven by variable speed motor 31, is determined by the maximum allowable temperature of the re-circulated gas 16 as measured by thermocouple 32, which must not exceed the temperature rating of the blower, which is generally about 2000F.
  • Item 33 is the seal and bearing area of the blower housing 20; the arrangement of this is well known in the art, including materials, cooling slingers, gas purging, and any other means to insure a long life for blower impeller 19 and inner case 20.
  • FIG. 7 yet another embodiment of a pressurized gasifier 16 is shown.
  • fuel 1 is periodically fed to a holding hopper 4 using a conveyor 2.
  • a level probe 3 determines when the hopper 4 is full to shut off the conveyor 2.
  • Another level probe 5 measures material level in a lock hopper 6.
  • a discharge dome valve 8 is closed and the hopper 6 is decompressed by opening valve 7, and then dome valve 9 opens to allow fuel 1 from the filled chute hopper 4 to rapidly fill lock hopper 6. Just enough material is added to chute hopper 4 each fill cycle to refill hopper 6.
  • Hopper 4 can have air inlets 10 (one shown) to prevent any suction effects from the rapid flow of material out of hopper 4 from flowing through valve 9, and/or vibrators 11 (one shown) to assist the rapid discharge of hopper 4. Hopper 4 can also be lined with HDPE plastic sheet to facilitate flow. When the hopper 4 is emptied (and hopper 6 is refilled), valve 9 is closed, hopper 6 is re- pressurized with gas via valve 14.
  • the gas could be air, CO2, nitrogen, or any other suitable gas applicable to the gasifier design.
  • valve 8 is reopened so unloader drive 12 can begin to rapidly unload hopper 6 of material 20 to replenish fuel zone 18 inside the gasifier 16, now at a lower level due to the refill time interval for hopper 6 to reestablish upper level 17 as measured by level probe, which can be a radar probe.
  • hopper 6 has an unloader so as to be able to handle a larger range of material, and it consists of electric motor gear head drive 12 supported by channel iron supports 13, the speed of drive 12 is controlled by the level probe 15. The lower the level 17 of upper feed zone 18 of gasifier 16, the faster the drive 12 is operated to refill zone 18 faster.
  • Drive 12 has a double ended shaft to both drive a top circular disk 19 which orientates material 20 and prevents uncontrolled flow through opening 22.
  • Plate 23 has a helical shaped leading edge cut so as to spiral material into the opening 22.
  • the material 20 flows through a chute 31 into the fuel zone 18.
  • the level of material in zone 18 is allowed to drop while the lock hopper 6 is being refilled by hopper 4. This simplifies the feed arrangement and takes maximum advantage of the fresh fuel zone 18, the level surge of which will have no deleterious effects on gasifier operation since this is the fresh fuel zone 18 where essentially no gasification is taking place.
  • the gasifier 16 has a re-circulating blower 23 driven by a variable speed motor 24 and re-circulation tubes 29 and 30 formed in the wall of the gasifier shell and running lengthwise therein.
  • Air injection valves 28 (one shown) enables the re-circulation tubes 29 and 30, respectively, to periodically be burned free of accumulating soot matter.
  • Level 34 is created by virtue that the gasified material 35 is moving down through the gasifier inner space generally seeking the angle of repose shown due to the chute 31 being offset from the center of the gasifier shell.
  • the temperature of the exit gas 36 is measured by thermocouples 37, and the speed of blower motor 24 is sufficient to pull hottest lower gases 38 at a rate up though the whole fuel mass 35 such that gases 36 and 33 are of sufficient temperature (generally over 1600F) to be free of tars.
  • the blower wheel (not shown) of blower 23 is cooled and steam cleaned by flows (not shown) via a double ported rotary valve 27.
  • the temperature of gas 33 leaving the blower 23 is also measured (sensor not shown) to insure the blower is not overheated, although as noted it is cooled by coolant flows though 27.
  • Gasifier 16 is generally highly pressurized (although it can be an atmospheric pressure blown gasifier) and gas 36 leaves through tuyeres 39 (only one shown).
  • the temperature of gas 36 can also be influenced or controlled by how much hot gas 33 circulates through bypass three way valves 40 and 41 respectively, thus how much enters lower tubes 44 and 45 respectively to burn in fire zone 46, increasing the temperature of the hot fire zone 46.
  • Steam injection 47 (only one shown) can also be used to assist in controlling the temperatures of gases 33 and 36.
  • valve 41 is inserted in rammed refractory 49 (which can alternatively be a water wall) to intersect gas flow though tubes 29 and 30 respectively.
  • Valve 41 has an operator 50 on one end with a shaft 51 stuffing box (not shown) to accommodate the gasifier pressure.
  • the shaft 51 is attached to sliding ceramic block 52 causing it to slide in or out horizontally as needed.
  • Block 52 has a through opening 53 to allow gases 55 to pass through down to the lower tube area 45, but also has a wedged shaped inner end 54, which if the block 52 is pushed all the way in by operator 50, will block off all the upper gas flow 43 and all gas 33 in tube 30 flows at 55 to make a hotter fire in zone 46.
  • the steam in gas 33 from drying fuel 1 is uniquely positioned whether as flow 43 or 55 to enhance gasification reactions in zone 46 and has the effect to reduce the steam flow 47.
  • re-circulating gas flow 33 in this way has the effect of achieving similar gasification efficiency as if fuel 1 were dry since 30-40% of dry fuel mass 1 must be steam addition to gasify properly, and this steam is made from extra dry fuel added.
  • fuels as wet as 40% will not appreciably affect the overall thermal efficiency of the gasifier or result in any more fuel 1 to be added on a dry measured basis (more weight of fuel 1 is of course added than dry fuel on a wet basis).
  • Valve 40 is designed to operate the same way as 41.
  • valve block 52 does not need to be a tight fit within valve 41 to perform its intended function. Generally, not over thirty to forty inches of water backpressure is expected from fire zone 46 up through hot zone 32.
  • the lower area of zone 18 will be where coal caking occurs, thus the lower stirrer 27 serves to break up this caking. It's in zone 18 that the volatile compounds are driven off and enter with gas flow 33 whereby temperature in this area 32 are maintained high enough to insure the gas 33 is also free of tars along with the exit gas 36, i.e. the gas 33 is at least 1600F or higher in temperature to avoid tars in either gases 33 and 36. There are ample means to control the upper temperature of these gases 33 and 36.
  • Gasifier 16 as shown is a slagging gasifier, but it could be non- slagging as well using an ash unloader as described for the feed lock hopper 6 with rotating components water cooled.
  • the slagging discharge lock hopper is not shown.
  • the two oxidant blasts 56 and 57, respectively, are maintained of sufficient flow to maintain an exit gas 36 having a CO2 concentration to about 5% (CO2 measurement instrument is not shown but would be a pressure reducing gas sampling device to an atmospheric CO2 probe taken near temperature sampling area 37) and at the least hot enough temperature in zone 46 such that slag 58 flows around baffle 59 and out tap hole 60 into a slag quenching and lock hopper (not shown).
  • thermocouples 48 (only one shown) in zone 46 would generally be gas-cooled thermocouples with at least two installed, with one as a backup.
  • zone 46 is not high enough in temperature to maintain molten slag 58 conditions, flux agents can also be added with fuel 1, or as noted, the induction coil 61 can be designed into the base of the tap hole 60.
  • the separate tube 66 denoted by a dotted line allows steam flow made from quenching the slag in the quench tank space (not shown) to be separately introduced into the void space 65 which, and due to the suction created by the high velocity flows 57 and 55, which could have adjustable nozzles, will suction this steam away from the tap hole discharge end.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention concerne un gazéificateur qui inclut une enveloppe de gazéificateur, un moyen permettant d'introduire du carburant dans l'enveloppe, et un moyen permettant d'introduire un oxygénate dans l'enveloppe. Le gazéificateur inclut également un moyen permettant de décharger du gaz à partir de l'enveloppe qui peut être placé en dessous du moyen permettant d'introduire l'oxygénate. Le gazéificateur peut également inclure un moyen permettant de faire re-circuler du gaz avant que le gaz soit déchargé de l'enveloppe.
PCT/US2007/020555 2006-09-22 2007-09-22 Gazéificateurs à carburant de masse WO2008039400A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US12/442,215 US20100107493A1 (en) 2006-09-22 2007-09-22 Bulk fueled gasifiers

Applications Claiming Priority (6)

Application Number Priority Date Filing Date Title
US84679006P 2006-09-22 2006-09-22
US60/846,790 2006-09-22
US85094406P 2006-10-11 2006-10-11
US60/850,944 2006-10-11
US87548306P 2006-12-18 2006-12-18
US60/875,483 2006-12-18

Publications (1)

Publication Number Publication Date
WO2008039400A1 true WO2008039400A1 (fr) 2008-04-03

Family

ID=39230508

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2007/020555 WO2008039400A1 (fr) 2006-09-22 2007-09-22 Gazéificateurs à carburant de masse

Country Status (2)

Country Link
US (1) US20100107493A1 (fr)
WO (1) WO2008039400A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010028203A2 (fr) * 2008-09-04 2010-03-11 Econo-Power International Corp. Appareil de gazéification sous pression permettant de convertir du charbon ou un autre matériau carboné en gaz tout en produisant une quantité minimale de goudron
CN101592335B (zh) * 2009-06-30 2011-05-18 刘善华 烟梗废弃物气化系统装置及其生产工艺

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10011792B2 (en) * 2010-08-16 2018-07-03 Nikhil Manubhai Patel Sandwich gasification process for high-efficiency conversion of carbonaceous fuels to clean syngas with zero residual carbon discharge
CN102322645B (zh) * 2011-10-08 2013-04-24 张务谨 锅炉供热系统装置
KR101218976B1 (ko) * 2012-06-26 2013-01-09 한국에너지기술연구원 가변형 가스화기가 구비된 발전과 연소보일러 겸용 가스화 장치 및 그 운전방법
US20150107496A1 (en) * 2013-10-18 2015-04-23 Krishna Kumar Bindingnavale Ranga Biomass gasifier system for power generation
JP6762715B2 (ja) * 2015-12-28 2020-09-30 松下　靖治 ガス化炉
US11976246B1 (en) * 2023-02-10 2024-05-07 Conversion Energy Systems, Inc. Thermal conversion of plastic waste into energy

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020046886A1 (en) * 2000-03-30 2002-04-25 Jones David Lane Apparatus and method for weighing the occupant of a bed
US20060059870A1 (en) * 2004-09-23 2006-03-23 Beech James H Jr Process for removing solid particles from a gas-solids flow
US20060157899A1 (en) * 2005-01-15 2006-07-20 Lew Holdings, Llc Single vessel blast furnace and steel making/gasifying apparatus and process

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2324053A1 (fr) * 2000-10-20 2002-04-20 Malahat Systems Corporation Gazeifieur

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20020046886A1 (en) * 2000-03-30 2002-04-25 Jones David Lane Apparatus and method for weighing the occupant of a bed
US20060059870A1 (en) * 2004-09-23 2006-03-23 Beech James H Jr Process for removing solid particles from a gas-solids flow
US20060157899A1 (en) * 2005-01-15 2006-07-20 Lew Holdings, Llc Single vessel blast furnace and steel making/gasifying apparatus and process

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010028203A2 (fr) * 2008-09-04 2010-03-11 Econo-Power International Corp. Appareil de gazéification sous pression permettant de convertir du charbon ou un autre matériau carboné en gaz tout en produisant une quantité minimale de goudron
WO2010028203A3 (fr) * 2008-09-04 2010-10-21 Econo-Power International Corp. Appareil de gazéification sous pression permettant de convertir du charbon ou un autre matériau carboné en gaz tout en produisant une quantité minimale de goudron
US9587186B2 (en) 2008-09-04 2017-03-07 Epic Clean Technologies Corporation Pressurized gasification apparatus to convert coal or other carbonaceous material to gas while producing a minimum amount of tar
CN101592335B (zh) * 2009-06-30 2011-05-18 刘善华 烟梗废弃物气化系统装置及其生产工艺

Also Published As

Publication number Publication date
US20100107493A1 (en) 2010-05-06

Similar Documents

Publication Publication Date Title
US20100107493A1 (en) Bulk fueled gasifiers
JP6402419B2 (ja) 供給原料をガス化するための方法およびデバイス
US10465133B2 (en) Device with dilated oxidation zone for gasifying feedstock
US8546636B1 (en) Method for gasifying feedstock
US10662386B2 (en) Method for gasifying feedstock with high yield production of biochar
CA2530236A1 (fr) Bruleur a combustion gazeifiant a cyclone haute efficacite pour la production d'energie thermique et dispositifs et methodes d'utilisation
JP5198737B2 (ja) 粒子状廃棄物ガス化システム及び方法
BR112013009116B1 (pt) instalação e método de tratamento de resíduo
JP2007126625A5 (fr)
RU2084493C1 (ru) Способ газификации твердого топлива, способ газификации угля и устройства для их осуществления
JPH08337447A (ja) 竪型焼成炉
US11566191B2 (en) System and process for continuous production of contaminate free, size specific biochar following gasification
US20210317374A1 (en) Updraft gasifier and method, apparatus, and system for biomass decomposition
WO2021061171A1 (fr) Procédé de gazéification d'une charge d'alimentation avec une production à rendement élevé de biocharbon
WO2011057040A2 (fr) Cokéfaction continue sous pression par combustion directe
JP2004143204A (ja) 固形バイオマス燃料のガス化装置
JP3957526B2 (ja) 固形燃料や有機物のガス化装置
WO2010123444A1 (fr) Procédé et installation pour brûler du combustible solide
JP6943489B1 (ja) バイオマスバーナー
JP2004256598A (ja) 可燃物のガス化方法及び装置並びにガス化溶融システム
KR100978349B1 (ko) 보일러
JPH09243017A (ja) 流動層熱反応炉への可燃物供給装置
GB190629408A (en) Improvements in Cement Kilns.
OA17533A (en) Method and device for gasifying feedstock.

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 07838707

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 07838707

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 12442215

Country of ref document: US